EP0753562A1 - Verfahren zur Umsetzung von Synthesegas in flüssiger Phase - Google Patents

Verfahren zur Umsetzung von Synthesegas in flüssiger Phase Download PDF

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Publication number
EP0753562A1
EP0753562A1 EP96401465A EP96401465A EP0753562A1 EP 0753562 A1 EP0753562 A1 EP 0753562A1 EP 96401465 A EP96401465 A EP 96401465A EP 96401465 A EP96401465 A EP 96401465A EP 0753562 A1 EP0753562 A1 EP 0753562A1
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EP
European Patent Office
Prior art keywords
liquid phase
hydrocarbons
catalyst
synthesis gas
reaction
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EP96401465A
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English (en)
French (fr)
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EP0753562B1 (de
Inventor
Patrick Chaumette
Pierre Boucot
Pierre Galtier
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IFP Energies Nouvelles IFPEN
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IFP Energies Nouvelles IFPEN
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
    • C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/02—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon
    • C07C1/04—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon from carbon monoxide with hydrogen
    • C07C1/06—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon from carbon monoxide with hydrogen in the presence of organic compounds, e.g. hydrocarbons

Definitions

  • the present invention relates to a process for synthesizing essentially C 5 + hydrocarbons (that is to say hydrocarbons comprising at least 5 carbon atoms per molecule), usable as fuel or liquid fuel, from gases of synthesis.
  • the synthesis gas is a CO- (CO 2 ) -H 2 mixture, that is to say a CO-H 2 mixture of carbon monoxide (CO) and hydrogen (H 2 ) optionally comprising carbon dioxide carbon (CO 2 ).
  • the reaction for the synthesis of hydrocarbons from synthesis gas generally carried out at a temperature between 150 and 350 ° C. and under pressure, is known under the name of Fischer-Tropsch synthesis.
  • the catalysts usually used for the transformation of CO- (CO 2 ) -H 2 mixtures into liquid or gaseous hydrocarbons generally comprise at least one group VIII metal such as iron, ruthenium, cobalt or nickel.
  • the products prepared by Fischer-Tropsch synthesis in the presence of these metal catalysts have a very wide distribution in terms of molecular weight. Thus only a small proportion of the products obtained is in the range of middle distillates constituted by kerosene and diesel fractions, the kerosene fraction (s) being constituted by a mixture of hydrocarbons whose points of boiling are approximately between 140 and 300 ° C, and the diesel fraction (s) being constituted (s) by a mixture of hydrocarbons whose boiling points are approximately between 180 and 370 ° C during '' atmospheric distillation as carried out on a crude oil by a person skilled in the art.
  • the reaction which it is sought to carry out in the context of the present application is the reaction for the synthesis of essentially C 5 + hydrocarbons from synthesis gas.
  • the Fischer-Tropsch synthesis is a very exothermic reaction. So that when the process for carrying out said synthesis reaction is carried out in the gas phase and with a catalyst in a fixed bed, the conversion of carbon monoxide must be limited to less than 85%, in order to avoid instabilities thermal in the catalytic bed, which requires separation and recycling of the unconverted synthesis gas.
  • Another process which has been envisaged for carrying out the reaction consists in operating in the presence of a liquid phase and with a catalyst in suspension (circulating bed reactor also called “slurry").
  • a catalyst in suspension circulating bed reactor also called "slurry”
  • the CO conversion can reach or even exceed 95%.
  • the catalyst suspended and circulating with the inert liquid must be separated from the reaction products, then recycled.
  • the object of the present invention is to provide a process which avoids the disadvantages of fixed bed / gas phase and circulating bed processes, and which makes it possible to preserve the advantages of a fixed bed reactor with downward flows of the liquid and the gas, while more particularly favoring the formation of C 5 + hydrocarbons compared to the formation of methane.
  • the process of the present invention is a process for synthesizing essentially linear and saturated C 5 + hydrocarbons from synthesis gas, the reactive gas phase circulating either in the downward direction or in the upward direction through a reaction zone.
  • comprising a fixed catalyst bed said method being characterized in that it comprises the upward circulation through said zone of an inert liquid phase, with a surface speed greater than 0.01 cm / s, preferably greater than 0, 1 cm / s and even more preferably greater than 1 cm / s.
  • the method according to the invention is also called "trickle bed upflow".
  • the surface velocity of the inert liquid phase is defined as the ratio between the hourly volume velocity, under the temperature and pressure conditions selected for the reaction, and the cross-sectional area of the reaction zone, said zone being considered without catalyst.
  • the optimum surface speed depends in part on the size of the catalyst particles and the physicochemical properties of the liquid. It seems practically independent of the surface velocity of the gas.
  • the reaction zone comprises one or more reactors, each reactor comprising at least one fixed bed of catalyst. In the case where the reaction zone comprises several reactors, these can be placed in series or in parallel. In all cases, the configuration of the reaction zone is carried out in a manner well known to those skilled in the art.
  • the catalyst particles generally have an average diameter of between 0.2 and 10 mm, preferably between 0.5 to 6 mm and more preferably between 1 and 3 mm.
  • the catalyst can be any type of catalyst which is effective in the reaction for the synthesis of hydrocarbons from synthesis gas.
  • any catalyst based on iron or on cobalt, supported or not such as those described in European patent application EP-A-0,581,619 and in French patent FR-A-2,677,992.
  • the liquid phase does not take part in the reaction and has no harmful effect on the latter. It is preferably a hydrocarbon cut, even more preferably comprising essentially between 10 and 20 carbon atoms per molecule, such as a diesel cut or a kerosene cut. If the catalyst is sensitive to sulfur, a desulfurized hydrocarbon cut is preferably used.
  • the liquid phase is preferably partially vaporizable under the conditions of the reaction, so as to eliminate the calories released by the reaction.
  • the liquid phase comprises at least one partially vaporizable product, for example between 0 and 80% of an at least partially vaporizable product.
  • vaporizable is understood to mean any liquid product which, under the conditions of the reaction, is practically completely in the form of gas.
  • partially vaporizable product means a product of which a portion, generally between 10 and 100%, is vaporizable.
  • the liquid phase comprises a partially vaporizable hydrocarbon fraction, for example a hydrocarbon fraction comprising hydrocarbons containing 5, 6, 7, 8, 9 or 10 carbon atoms per molecule.
  • the inert liquid phase is advantageously obtained by recycling part of a fraction of the hydrocarbons produced by the reaction; of preferably said fraction is the diesel or kerosene fraction of the hydrocarbons produced by the reaction.
  • the inert liquid phase which is initially introduced into the reaction zone is supplied from the outside (as opposed to a liquid phase produced in the Fischer-Tropsch reaction zone, that is to say at the interior), then said liquid phase comprises part of a fraction of the hydrocarbons produced by the reaction which is recycled in said zone.
  • said fraction is the diesel fraction or the kerosene fraction.
  • the inert liquid phase generally has a density between 0.2 and 2.5 g / cm 3 and a viscosity between 0.05 and 10 centipoise (0.05 to 10 mPa.s) under the conditions of reaction, but these values are by no means mandatory.
  • the process according to the invention is particularly well suited to be used as a process for manufacturing from a synthesis gas a mixture of essentially linear and saturated hydrocarbons, generally containing at least 80% by weight, relative to all of the hydrocarbons formed, of a cut comprising C 5 + hydrocarbons and preferably less than 10% by weight of olefins in said C 5 + cut.
  • the process according to the invention therefore makes it possible to obtain essentially paraffinic hydrocarbons, the fraction of which exhibiting the highest boiling points can be converted with a high yield into middle distillates (diesel and kerosene cuts) by a hydroconversion process. such as hydrocracking and / or catalytic hydroisomerization (s).
  • the conversion of synthesis gas to hydrocarbons is generally carried out under a total pressure of between 0.1 and 15 MPa, preferably between 0.5 and 10 MPa, the temperature being between 150 and 350 ° C, preferably between 180 and 270 ° C.
  • the hourly volume speed is usually between 100 and 20,000 volumes of synthesis gas per volume of catalyst per hour and preferably between 400 and 10,000 volumes of synthesis gas per volume of catalyst per hour.
  • the H 2 / CO molar ratio in the synthesis gas is generally between 0.5 and 5, preferably between 1.2 and 3.5.
  • the catalyst is first of all loaded in the reaction zone and prereduced by contacting at least one reducing compound, for example pure hydrogen or a mixture of reducing gases. such as hydrogen and / or carbon monoxide, and optionally an inert gas such as nitrogen, the molar ratio (reducing compound) :( reducing compound + inert gas) being between 0.001: 1 and 100: 1 in the case where at least one inert gas is present.
  • the pre-reduction is generally carried out between 150 and 600 ° C, preferably between 200 and 500 ° C, between 0.1 and 10 MPa, and at an hourly volumetric speed of 100 to 40,000 volumes of mixture per volume of catalyst and per hour .
  • This pre-reduction is optionally carried out in the liquid phase, the liquid phase of the pre-reduction for example consisting of at least one hydrocarbon comprising at least 5 carbon atoms per molecule.
  • the catalyst used in Examples 1 to 4 is prepared as follows:
  • the gel obtained is separated from the mother liquors by filtration, washed with water, dried in an oven between 40 and 120 ° C, then calcined at 450 ° C and shaped by tableting. the 5x5mm size pellets are then recalcined at 600 ° C.
  • the catalyst is reduced in the reactor, prior to the synthesis of hydrocarbons, by means of a mixture containing 6% hydrogen in nitrogen, up to 240 ° C., then by pure hydrogen up to 500 ° C, at atmospheric pressure.
  • Example 1 (according to the invention):
  • the synthesis gas (mixture H 2 + CO, line 1) and the liquid phase (line 2 ) flow from bottom to top and pass through 1.2 dm3 of the catalyst ( 3 ) mentioned. above and placed in a fixed bed in reactor 4 .
  • the liquid is distributed uniformly through a perforated plate ( 5 ).
  • the effluent is discharged by means of the pipe ( 6 ).
  • the liquid paraffins are separated from the gas phase, at the outlet of the reactor, in the separator ( 7 ), and sent continuously by the line ( 8 ) to the heater ( 10 ), up to the separator 11 .
  • the gas from the separator 7 is removed by means of line 9 and analyzed by chromatography.
  • the heavy paraffins synthesized in the reactor 4 are separated and then recovered via line 13 ; they are analyzed by chromatography.
  • a gaseous phase is recovered which, after passing through condenser 14 , condenses into the liquid phase recycled to reactor 4 via pump 15 and line 2 .
  • the reactor has a diameter of 4 cm and a height of 1 meter.
  • the synthesis gas used for the synthesis of hydrocarbons consists of a mixture containing 66.7% of hydrogen and 33.3% of carbon monoxide.
  • the gas is introduced with a flow rate of 1.2 m 3 / h, i.e. a gas VVH (hourly volume speed) of 1000 h -1 .
  • the reaction is carried out at 220 ° C and 2MPa.
  • the liquid phase is a C 10 -C 16 paraffin cut containing no sulfur which is introduced at the start of the unit, then separated from the effluents at the outlet of the reactor, and then recycled.
  • the flow rate of this liquid phase is approximately 200 l / h at the reaction temperature, ie a space speed of 4.5 cm / s. Products lighter or heavier than this liquid phase, as well as the water co-produced in the reaction, are separated, evacuated and analyzed.
  • C1, C2, C3, ... Cn the number of gram-molecules of carbon monoxide CO and carbon dioxide CO 2 (if CO 2 is present) transformed into hydrocarbons containing from 1 to n atoms of carbon per molecule.
  • the conversion is 72%
  • the selectivity for methane is 8%
  • the selectivity for C 5 + hydrocarbons is 86%.
  • the reaction is carried out under conditions identical to those of Example 1 except for the space velocity of the liquid phase which is 1 cm / s.
  • the reaction is carried out under conditions identical to those of Example 1 except for the gas phase which circulates from top to bottom with the same VVH equal to 1000 h-1.
  • the synthesis gas (mixture H 2 + CO, line 1) flows from top to bottom and the liquid phase (line 2 ) flows from bottom to top; the two phases pass through 1.2 dm3 of the catalyst ( 3 ) mentioned above and placed in a fixed bed in the reactor 4 .
  • the other references of FIG. 2 are those of FIG. 1.
  • the reaction is carried out under conditions identical to those of Example 1 except for the liquid and gas phases which both flow from top to bottom.
  • the synthesis gas (mixture H 2 + CO, line 1 ) and the liquid phase (line 2 ) both flow from top to bottom and pass through 1.2 dm3 of the catalyst ( 3 ) mentioned above and placed in a fixed bed in reactor 4 .
  • the other references of FIG. 3 are those of FIG. 1.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Catalysts (AREA)
EP96401465A 1995-07-13 1996-07-03 Verfahren zur Umsetzung von Synthesegas in flüssiger Phase Expired - Lifetime EP0753562B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR9508637A FR2736650B1 (fr) 1995-07-13 1995-07-13 Procede de conversion du gaz de synthese en phase liquide
FR8600037 1995-07-13

Publications (2)

Publication Number Publication Date
EP0753562A1 true EP0753562A1 (de) 1997-01-15
EP0753562B1 EP0753562B1 (de) 1999-12-15

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EP96401465A Expired - Lifetime EP0753562B1 (de) 1995-07-13 1996-07-03 Verfahren zur Umsetzung von Synthesegas in flüssiger Phase

Country Status (8)

Country Link
US (1) US5786393A (de)
EP (1) EP0753562B1 (de)
DE (1) DE69605607T2 (de)
FR (1) FR2736650B1 (de)
MY (1) MY112375A (de)
NO (1) NO314697B1 (de)
SA (1) SA96170191B1 (de)
ZA (1) ZA965836B (de)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108579639A (zh) * 2018-04-03 2018-09-28 浙江新和成股份有限公司 一种制备氧代异佛尔酮的装置及方法

Families Citing this family (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6616909B1 (en) * 1998-07-27 2003-09-09 Battelle Memorial Institute Method and apparatus for obtaining enhanced production rate of thermal chemical reactions
WO2000034414A1 (en) 1998-12-07 2000-06-15 Syntroleum Corporation Structured fischer-tropsch catalyst system and method for its application
BR0013344A (pt) * 1999-08-17 2002-06-04 Battelle Memorial Institute Estrutura de catalisador e processo de sìntese de fischer-tropsch
US6451864B1 (en) * 1999-08-17 2002-09-17 Battelle Memorial Institute Catalyst structure and method of Fischer-Tropsch synthesis
GB0129054D0 (en) * 2001-12-05 2002-01-23 Accentus Plc Catalytic reactor and process
BR0206966A (pt) * 2001-12-05 2004-03-09 Accentus Plc Processo para realizar reforma de vapor/metano para gerar monóxido de carbono e hidrogênio, e, planta para processar metano
RU2210432C1 (ru) * 2001-12-21 2003-08-20 Институт катализа им. Г.К. Борескова СО РАН Катализатор и способ получения углеводородов и их кислородсодержащих производных из синтез-газа
US7232848B2 (en) * 2002-09-09 2007-06-19 Conocophillips Company Gas agitated multiphase reactor with stationary catalyst solid phase
MY139252A (en) * 2004-10-04 2009-09-30 Shell Int Research Catalyst structure
CN101307245B (zh) * 2008-05-19 2012-08-22 中国科学院山西煤炭化学研究所 一种利用固定床装置进行费托合成反应的工艺及设备
CN101275080B (zh) * 2008-05-19 2012-11-14 中国科学院山西煤炭化学研究所 一种基于固定床反应器的费托合成反应工艺
CN101928194B (zh) * 2009-06-18 2013-06-05 中国石油化工股份有限公司 一种固定床费托合成的方法
CN102211002B (zh) * 2010-04-12 2013-03-27 中科合成油技术有限公司 一种热油循环和冷激式固定床费托合成反应器及其应用
CN103695024B (zh) * 2013-12-09 2016-01-27 中国科学院山西煤炭化学研究所 一种适用于滴流床反应器的费托合成工艺
CN103691369B (zh) * 2013-12-09 2015-10-28 中国科学院山西煤炭化学研究所 一种基于固定床反应器的费托合成工艺

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE897549C (de) * 1939-04-01 1953-11-23 Basf Ag Verfahren zur katalytischen Umsetzung von Kohlenoxyd mit Wasserstoff zu Kohlenwasserstoffen
GB728543A (en) * 1952-03-05 1955-04-20 Koppers Gmbh Heinrich Process for the synthesis of hydrocarbons
NL7708307A (en) * 1977-07-27 1979-01-30 Shell Int Research Fischer-Tropsch hydrocarbon synthesis - using catalyst contg. ruthenium and iron-group metal
US4413063A (en) * 1980-11-25 1983-11-01 Institut Francais Du Petrole Process for operating highly exothermic reactions
EP0188304A1 (de) * 1985-01-18 1986-07-23 Shell Internationale Researchmaatschappij B.V. Verfahren zur Herstellung von Kohlenwasserstoffen

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE897549C (de) * 1939-04-01 1953-11-23 Basf Ag Verfahren zur katalytischen Umsetzung von Kohlenoxyd mit Wasserstoff zu Kohlenwasserstoffen
GB728543A (en) * 1952-03-05 1955-04-20 Koppers Gmbh Heinrich Process for the synthesis of hydrocarbons
NL7708307A (en) * 1977-07-27 1979-01-30 Shell Int Research Fischer-Tropsch hydrocarbon synthesis - using catalyst contg. ruthenium and iron-group metal
US4413063A (en) * 1980-11-25 1983-11-01 Institut Francais Du Petrole Process for operating highly exothermic reactions
US4529738A (en) * 1980-11-25 1985-07-16 Institut Francais Du Petrole Process for operating highly exothermic reactions
EP0188304A1 (de) * 1985-01-18 1986-07-23 Shell Internationale Researchmaatschappij B.V. Verfahren zur Herstellung von Kohlenwasserstoffen

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108579639A (zh) * 2018-04-03 2018-09-28 浙江新和成股份有限公司 一种制备氧代异佛尔酮的装置及方法
CN108579639B (zh) * 2018-04-03 2024-01-30 浙江新和成股份有限公司 一种制备氧代异佛尔酮的装置及方法

Also Published As

Publication number Publication date
ZA965836B (en) 1998-01-12
DE69605607T2 (de) 2000-04-13
SA96170191B1 (ar) 2006-04-22
EP0753562B1 (de) 1999-12-15
FR2736650A1 (fr) 1997-01-17
DE69605607D1 (de) 2000-01-20
NO962930L (no) 1997-01-14
NO962930D0 (no) 1996-07-12
FR2736650B1 (fr) 1997-09-05
NO314697B1 (no) 2003-05-05
MY112375A (en) 2001-05-31
US5786393A (en) 1998-07-28

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